Production of cyclic acetals or ketals using solid acid catalysts

ABSTRACT

A process for making a cyclic compounds such as cyclic acetal or cyclic ketones by feeding aldehyde or ketone compounds and polyhydroxyl compounds to a reaction zone at a molar ratio of polyhydroxyl compounds to aldehyde or ketone compounds of at least 3:1, reacting these compounds in the presence of a solid acid such as an acidic ion exchange resin, to generate a liquid reaction mixture without separating water from the reaction mixture as it is being formed in the reaction mixture, withdrawing the liquid reaction mixture from the reaction zone as a liquid product stream, and feeding the liquid reaction product stream to a distillation column to separate cyclic acetal compounds from unreacted polyhydroxyl compounds, and optionally recycling back the unreacted polyhydroxyl compounds to the reaction zone. The process produces cyclic acetal compounds in yields of at least 90% with long catalyst life. The process is also suitable to make cyclic ketals from ketone compounds.

1. FIELD OF THE INVENTION

The invention relates to the production of cyclic acetals or ketals athigh yields and long catalyst life.

2. BACKGROUND OF THE INVENTION

Ether alcohols, such as 2-butoxyethanol, have important industrialfunctions in products such as cleaning supplies and coating materials.In the past, the manufacture of these products has been based on aprocess relying on a reaction between an alcohol and ethylene oxide.This conventional process has proven to be somewhat inefficient, in thatit produces various undesirable byproducts along with the etheralcohols.

Monoether glycols can also be manufactured in a reaction betweenaliphatic aldehydes and ethylene glycol, instead of ethylene oxide,under acidic conditions in order to produce cyclic acetals. The acetalof ethylene glycol and butyraldehyde, for example, is described byHibbert and Timm (Hibbert, H.; Timm, J. A. J. Am. Chem. Soc. 1924,46(5), 1283-1290) and is achieved with a maximum yield of 50%. Thesecyclic acetals, or ketals when a ketone is substituted for the aldehyde,can then be subjected to hydrogenolysis in the presence of palladium andphosphoric acid catalysts. Such a process is described in U.S. Pat. No.4,484,009.

The reaction of the polyhydroxyl compounds with aldehydes or ketones isan equilibrium reaction with the acetal product and by-product water.Yield of acetal or ketal is reduced via hydrolysis of the acetal by theco-product water. Thus, it is desirable to remove water from thereaction system to increase yield of the acetal.

The separation of water from the reaction mixture has been difficultsince it often forms an azeotrope with the aldehyde reactants and withthe cyclic acetal products. Entrainers have been employed to removewater through azeotropic distillation. Sulzbacher and coworkers, forexample, describe removing the water by using benzene during thepreparation of a number of acetals of ethylene glycol (Sulzbacher, M.et. al. J. Am. Chem. Soc. 1948, 70(8), 2827-2828). The environmental andhealth impact of benzene is an obvious concern in this method.Dessicants such as calcium chloride (DE 419223; Brønsted and Grove J.Am. Chem. Soc. 1930, 52(4), 1394-1403) may be employed in the reactionvessel to remove water as it is formed, but disposal of the generatedsolid waste is an economic and environmental concern.

Another method as described by Astle and coworkers, involves heating theglycol and aldehyde over an heterogeneous acidic resin and distillingout the acetal and water as they are formed (Astle, M. J. et al, Ind.Eng. Chem. 1954, 46(4), 787-791). This method generally had low yieldswith one example for the manufacture of 2-butoxyethanol reported ashaving a yield of about 92% using a molar ratio of ethylene glycol tobutyraldehyde of about 1.3:1. In these reactions, water was beingseparated from the reaction mixture in the flask as the water was beingformed, and upon completion, the reaction mixture in the flask wasfiltered and phase separated. The removal of water from the reactionmixture as it was being formed follows from the understanding that thereaction of the polyhydroxyl compounds with aldehydes is an equilibriumreaction with the acetal product and by-product water, and the yield ofacetal is reduced via hydrolysis of the acetal by the co-product wateror can be increased with the removal of water as it is formed.

One pot reaction systems have also been reported, that is, reacting analdehyde and a polyhydroxyl with hydrogen in the presence of a noblemetal catalyst directly to the desired ether alcohol. For example, U.S.Pat. No. 5,446,210 describes a process for the production of hydroxyether hydrocarbons in a one pot system by reacting a polyhydroxyl withan aldehyde and hydrogen in the presence of a noble metal catalyst wherethe molar ratio of polyhydroxyl to aldehyde compound ranges from 5:1 to1:5 is described, but with these molar ratios, the yield was low in therange of 35 to 50% when including the bis-types of by-products with lowselectivity to the mono-ether products.

US Publication No. 2010/0048940 also describes a one pot system in whicha polyhydroxyl and a aldehyde compound and hydrogen are reacted togetherin the presence of a hydrogenolysis catalyst to provide the polyhydroxylether, where the molar ratio of polyhydroxyl to aldehyde exceeds 5:1 toimprove selectivity and yield. An example of a two stage process inwhich the acetal compound was first synthesized and then subjected tohydrogenolysis was reported without describing the yield value of theacetal produced, although the yield to the 2-butoxyethanol byhydrogenolysis of the acetal was reported as having a selectivity ofabout 61%.

In U.S. Pat. No. 5,917,059 to BASF Aktiengesellschaft, the authorsgenerate cyclic acetals and ketals by reacting a molar excess ofaldehydes and ketones with polyhydroxyl compounds in the presence of anacid catalyst. The water is removed by continuously distilling unreactedaldehydes or ketone starting materials, thus co-distilling the formedwater in the water/aldehyde azeotrope, and further replacing thedistilled aldehyde or ketone with fresh aldehyde or ketone. Thealdehydes and ketones act not only as a reactant but also as a mediumfor transporting the water produced in the reaction. This methodrequires large excess of aldehyde (e.g. 4:1 molar ratio ofaldehyde:alcohol) to be successful.

Reactive distillation is employed in U.S. Pat. No. 6,015,875 and U.S.Pat. No. 7,534,922 B2 to generate low boiling acetals. The authors makeuse of heterogeneous acids in the packing of the column and feed lowboiling starting materials such as methanol, ethanol, formaldehyde, andacetaldehyde. The formed acetals are removed overhead above thedistillation reaction zone and the co-product water is removed below thedistillation reaction zone. This method limits the types of usablereactants to those producing materials that boil at a temperature lowerthan water.

As can be seen from the available literature, there exists a continuedneed to produce cyclic acetal or ketal compounds in high yield with along catalyst life using a simple economic process.

3. BRIEF SUMMARY OF THE INVENTION

Cyclic acetals and ketals can now be produced in high yield with a longlife non-exotic catalyst in a simple method which does not requireremoval of water as it is generated. Contrary to the expectation thatyields would be unacceptably low unless water is removed during itsformation as a by-product, the process of the invention allows one toreact all starting materials in the liquid phase in one reaction zone tomake a reaction mixture which is removed in the liquid phase andsubsequently distilled to produce the desired cyclic acetal or ketal inhigh yields.

There is now provided a continuous process for making a cyclic acetal orketal compounds comprising:

-   -   a. feeding a carbonyl composition comprising an aldehyde        compound, a ketone compound, or a combination thereof, and a        polyhydroxyl composition comprising a polyhydroxyl compound, to        a reaction zone at a molar ratio of all polyhydroxyl compounds        to all carbonyl compounds fed to the reaction zone of at least        3:1; and    -   b. reacting the carbonyl composition with the polyhydroxyl        compound in the presence of a solid acid to generate a liquid        reaction mixture comprising cyclic compounds, water, and        unreacted polyhydroxyl compounds; and    -   c. without separating water from the reaction mixture as it is        being formed in the reaction mixture, withdrawing the liquid        reaction mixture from the reaction zone as a liquid product        stream; and    -   d. feeding the liquid reaction product stream directly or        indirectly to a distillation column to separate cyclic compounds        from unreacted polyhydroxyl compounds and withdrawing from the        distillation column an overhead product stream and a bottoms        stream, wherein the overhead product stream comprises cyclic        compounds, unreacted polyhydroxyl compounds and water and is        rich in the concentration of cyclic compounds by moles relative        to the bottoms stream, and the bottoms stream comprises        unreacted polyhydroxyl compounds and is rich in the        concentration of unreacted polyhydroxyl compounds by moles        relative to the overhead product stream;    -   wherein the selectivity to cyclic compounds in the overhead        product stream is at least 90%.

The yield of cyclic acetal or ketal compounds taken in an overheadproduct stream can also be at least 90%.

In the process of the invention, one may also recycle to the reactionzone at least a portion of unreacted polyhydroxyl compounds withdrawnfrom the distillation column in the bottoms stream. Reaction by-productsother than water may also be withdrawn from the bottoms stream toproduce a polyhydroxyl rich stream and an organic by-product richstream, following which at least a portion of the polyhydroxyl compoundsin the polyhydroxyl rich stream can be recycled to the reaction zone.

4. BRIEF DESCRIPTION OF THE DRAWINGS

FIG. 1 is a process flow diagram for the production of cyclic acetal orketal compounds in a reaction zone followed by distillation, separation,and recycling a portion of polyhydroxyl compounds to the reaction zone.

5. DETAILED DESCRIPTION OF THE INVENTION

There is now provided a continuous process for making cyclic compounds.By a cyclic compound is meant a compound having a ring structure thathas two oxygen atoms in the ring structure that are single bonded to thesame carbon atom in the ring structure. The cyclic compounds can becyclic acetal compounds or cyclic ketal compounds. The cyclic compoundsare made by feeding carbonyl compounds and a polyhydroxyl compositioncomprising a polyhydroxyl compound, to a reaction zone at a molar ratioof all polyhydroxyl compounds and all aldehyde or ketone compounds fedto the reaction zone of at least 3:1. By carbonyl compounds is meantaldehyde compounds, ketone compounds (depending upon whether one desiresto make an acetal or ketal), or a mixture of the two.

The carbonyl composition fed to the reaction zone contains one or moretypes of aldehyde or ketone compounds. Aldehyde compounds contain atleast one aldehyde functionality. The aldehyde and ketone compounds canbe represented by the Formula I:

in which R¹ and R² are independently hydrogen or a C₁-C₅₀ alkyl, C₂-C₅₀alkenyl, aryl-C₁-C₅₀ alkyl, aryl-C₂-C₅₀ alkenyl-, or C₃-C₁₂ cylcoalkyl,and wherein R¹ and R² are optionally connected through one or morecarbon atoms, and wherein the alkyl, alkenyl, aryl, and cycloalkylgroups of R¹ and R² are optionally saturated or unsaturated, andbranched or unbranched or substituted or unsubstituted with 1, 2, or 3groups comprising —OH, halogen, dialkylamino, C₁-C₆ alkyl, aldehyde,ketone, carboxylic acid, ester, ether, alkynyl, dialkylamide, anhydride,carbonate, epoxide, lactone, lactam, phosphine, silyl, thioether, thiol,aryl, phenol, or combinations thereof; and wherein when one of R¹ or R²is hydrogen, the compound will be an aldehyde and wherein when neitherR¹ and R² are hydrogen the compound is a ketone.

The aldehyde compound may have, if desired, at least one aldehydefunctional group wherein the aldehyde carbon atom is bonded to a (i)branched or unbranched C₁-C₉ alkyl group or (ii) an aryl or alicyclicgroup which is optionally substituted with a branched or unbranchedC₁-C₉ alkyl group.

Examples of aldehyde compounds include, but are not limited to,benzaldehyde, acetaldehyde, propionaldehyde, butyraldehyde,isobutyraldehyde, pentaldehyde, 2-methylbutyraldehyde,3-methylbutyraldehyde, n-pentanal, isopentanal, hexyldehyde,heptaldehyde, 2-ethylhexyldehyde, octanal, nonanal, n-decanal,2-methylundecanal, lauryl aldehyde, myristyl aldehyde, cetyl aldehyde,stearyl aldehyde, behenyl aldehyde, glutaraldehyde, acrolein,crotonaldehyde, oleyl aldehyde, linoleyl aldehyde, linolenyl aldehyde,erucyl aldehyde, cinnamaldehyde, 1,3-cyclohexanedicarboxaldehyde,1,4-cyclohexanedicarboxaldehyde, and combinations thereof.

Examples of ketone compounds include, but are not limited to, acetone,methyl ethyl ketone (2-butanone), methyl propyl ketone (2-pentanone),methyl isopropyl ketone (3-methyl-2-butanone), methyl isobutyl ketone(4-methyl-2-pentanone), 2-hexanone, 2-heptanone (methyl amyl ketone),2-octanone, and acetophenone.

The polyhydroxyl composition fed to the reaction zone contains one ormore types of polyhydroxyl compounds. Polyhydroxyl compounds have atleast two hydroxyl (—OH) functionalities. The polyhydroxyl compounds maycontain ether or ester linkages in the longest carbon chain.

Suitable polyhydroxyl compounds for the present invention include, butare not limited to ethylene glycol, 1,2-propanediol, 1,3-propanediol,1,4-butanediol, 1,3-butanediol, 1,2-butanediol, 1,2-pentanediol,2,4-pentandiol, 2,2-dimethyl-1,3-propanediol, diethyleneglycol, andtriethyleneglycol, glycerin, trimethylolpropane, xylitol, arabitol, 1,2-or 1,3cyclopentanediol, 1,2- or 1,3-cyclohexanediol, and2,3-norbornanediol.

The cumulative amount of polyhydroxyl compounds and carbonyl compoundsfed to the reaction zone are at a molar ratio of polyhydroxyl compoundsrelative to carbonyl compounds (aldehyde or ketone compounds) of atleast 3:1, or at least 4:1, or more than 5:1, or at least 6:1, or atleast 7:1, or at least 8:1, or at least 9:1, or at least 10:1, or atleast 13:1. There is no particular upper limit. It is economicallydesirable to limit the amount of polyhydroxyl compounds that need to beseparated and recycled balanced against the need to use an excesssufficient to enhance selectivity and yield to the desired cyclic acetalor ketal. Practically, a molar ratio of polyhydroxyl compounds tocarbonyl compounds does not need to be more than 30:1, or not more than20:1, and even not more than 15:1.

The molar ratio of polyhydroxyl compounds to carbonyl compounds isdetermined by the total amount fed to the reaction zone. If a recyclestream of polyhydroxyl compounds is fed to the reaction zone, thisquantity should be factored into the molar ratio.

The polyhydroxyl composition and the carbonyl compounds composition maybe fed as separate streams or as a combined stream into the reactionzone. If viscosity variances between the two are sufficiently great, itis desirable to pre-mix at least a portion of the polyhydroxylcomposition with at least a portion of the carbonyl compounds toincrease the yield and improve the number of contact sites between thealdehyde or ketone functionalities and hydroxyl functionalities. Asshown in FIG. 1, a polyhydroxyl composition stream 1 and a carbonylcompound composition stream 2 are premixed in a mixing zone prior toentering reaction zone through a reactant feed stream 3. It is alsopossible to feed the recycle stream 10 containing unreacted polyhydroxylcompounds into the mixing zone to adequately mix and uniformly disperseor dissolve all the carbonyl compounds in the polyhydroxyl composition,especially if the polyhydroxyl composition has a significantly higherviscosity than the carbonyl composition.

Either or both the polyhydroxyl composition and the carbonyl compositionmay be pre-heated if the viscosity of either or both are too high toprovide satisfactory mixing or if either or both are solids at ambientconditions. The polyhydroxyl compounds and the carbonyl compounds shouldbe in the liquid state upon entry into the reaction zone.

Polyhydroxyl compounds and the carbonyl compounds fed to the reactionzone are reacted in the presence of solid acidic particles. Theparticles are in the solid phase (heterogeneous) dispersed in the liquidreaction medium under reaction conditions inside the reaction zone. Theacidic particles may be a fixed bed or may be dispersed and mobile andfed to the reaction zone separately or premixed into one or both of thepolyhydroxyl composition stream(s) 1, the carbonyl composition stream(s)2, the recycle stream(s) 10, or the reactant stream 3 fed to thereaction zone. To avoid having to filter the solids from the productstream, it is desirable to use a fixed catalyst bed. The reaction zoneis desirably liquid full and the reaction mixture in the reaction zoneflows in the direction of the feed entry points to the effluentlocations. In a horizontal vessel, this can be a horizontal flow fromleft to right or right to left depending on the feed/effluentconfiguration. In a vertically oriented vessel, this can be from top tobottom or bottom to top. In one embodiment, the reaction mixture insidethe reaction zone flows in an upward direction of bottom to top. Byhaving the feed entry points at or near the bottom of the reaction zoneand the effluent at the top of the reaction zone, better mixing isobtained and the residence time for contacting the solid acid isimproved.

The reaction zone can be contained in any suitable vessel. In oneembodiment, the reaction vessel is a pipe or tank having an L/D ratio ofmore than 1:1, or more than 2:1, or more than 3:1, or more than 4:1, ormore than 5:1, or more than 6:1, or more than 7:1, or more than 8:1, ormore than 9:1, or more than 10:1.

The reaction vessel may be mechanically agitated. Practically, thereaction vessel is not mechanically agitated, especially if a fixedcatalyst bed is employed. For example, a pipe loaded with solid acidcatalyst can be used without mechanical agitation, although if desiredthe pipe may contain weirs or baffles to provide turbulent flow inducedagitation. In a fixed bed design, the solid catalyst particles can beretained between a support plate and a bed limiter.

The reaction can proceed well under atmospheric pressure and at elevatedpressure. The pressure within the reaction zone can be at least 0.1 atm,or at least 0.5 atm, or at least 1 atm, or at least 1.05 atm, or atleast 1.1 atm, or at least 1.5 atm, or at least 2 atm, or at least 3atm, or at least 4 atm. For most applications, the pressure does notneed to exceed 10 atm, or exceed 5 atm, or exceed 3 atm, or exceed 2atm.

Inside the reaction zone, polyhydroxyl compounds react with carbonylcompounds to produce cyclic acetals or cyclic ketals or a mixturethereof, water, and by-products. The cyclic acetal, for purposes of thisdescription, is the desired principal product produced from the reactionof the starting aldehydes and starting polyhydroxyl compounds. Theprincipal product, the cyclic acetal, is the cyclic reaction product ofone mole of the starting aldehyde compound with one mole of the startingpolyhydroxyl compound releasing one mole of water. Examples ofby-products in reaction mixture to make cyclic acetals arealdehyde-aldehyde reaction products, polyhydroxyl-polyhydroxyl reactionproducts, the secondary reaction products between cyclic acetals withany other reactants or with itself, internal re-arrangement of thecyclic acetal ring and any further reaction products resulting from thering re-arrangement, or a combination thereof. Since a high molar excessof polyhydroxyl compound is used, unreacted polyhydroxyl compounds willalso be present in the reaction mixture. The reaction mixture may alsocontain unreacted aldehyde compounds.

The same applies to the production of cyclic ketals. The cyclic ketal,for purposes of this description, is the desired principal productproduced from the reaction of the starting ketones and startingpolyhydroxyl compounds. The principal product, the cyclic ketal, is thecyclic reaction product of one mole of the starting ketone compound withone mole of the starting polyhydroxyl compound releasing one mole ofwater. Examples of by-products in reaction mixture to make cyclic ketalsare ketone-ketone reaction products, polyhydroxyl-polyhydroxyl reactionproducts, the secondary reaction products between cyclic ketals with anyother reactants or with itself, internal re-arrangement of the cyclicketal ring and any further reaction products resulting from the ringre-arrangement, or a combination thereof. Since a high molar excess ofpolyhydroxyl compound is used, unreacted polyhydroxyl compounds willalso be present in the reaction mixture. The reaction mixture may alsocontain unreacted ketone compounds.

The yield of a product compound (not by-products or water), whether onedesires to determine the yield of cyclic compounds, an acetal compound,or a ketal compound, is determined by dividing the moles of productcompounds produced by the moles of reactant fed in the lowest molarquantity, multiplied by 100. For example, the yield of cyclic compoundsis determined by dividing the moles of cyclic compounds produced by themoles of corresponding aldehyde and/or ketone compounds fed, multipliedby 100. The yield of cyclic acetal compounds is determined by dividingthe moles of cyclic acetal compounds produced by the moles of aldehydecompounds fed, multiplied by 100. The yield of cyclic ketal compounds isdetermined by dividing the moles of cyclic ketal compounds produced bythe moles of ketone compounds fed, multiplied by 100.

Selectivity of cyclic compounds is determined by dividing the moles ofcyclic compounds produced by the moles of their respective aldehyde orketone compounds converted, multiplied by 100. Selectivity to the cyclicacetal is determined by dividing the moles of cyclic acetal compoundsproduced by the moles of aldehyde compounds converted, multiplied by100. Selectivity to the cyclic ketal is determined by dividing the molesof cyclic ketal compounds produced by the moles of ketone compoundsconverted, multiplied by 100.

Conversion to cyclic compounds is determined by dividing the moles ofcyclic compounds converted by the moles of the respective aldehyde orketone compounds fed, multiplied by 100. Conversion to cyclic acetals isdetermined by dividing the moles of cyclic acetal compounds converted bythe moles of aldehyde compounds fed, multiplied by 100. Conversion tocyclic ketals is determined by dividing the moles of cyclic ketalcompounds converted by the moles of ketone compounds fed, multiplied by100.

In the process of the invention, high yields of cyclic compounds areobtainable without the necessity of separating the by-product water fromthe reaction mixture as it is being formed in the reaction mixture. Eventhough the reaction is an equilibrium reaction with the presence ofwater having the capability to hydrolyze the acetal or ketal product andlower yield, the reaction of polyhydroxyl compounds in high molar excesswith aldehyde compounds in the presence of the solid acid keeps theselectivity and yield of cyclic acetal high. This has the advantage thatwater is not required to be removed by distillation or other means inthe reaction zone where the ion exchange catalyst is present and as itis being formed in order to obtain high yields. Further, the reactionprocessing window is widened and not constrained by the boiling pointranges of the reactants and reaction products and by-products.Furthermore, the catalyst life of solid acids is long and after 500hours of continuous operation does not need to be replaced orregenerated. In the process of the invention, the catalyst life (periodof time before catalyst activity diminishes by 30% from its activity asa fresh load) is at least 1 month, or at least 6 months, or at least 1year, or at least 2 years, or at least 3 years.

The cyclic reaction products formed in the reaction mixture contain anacetal moiety or a ketal moiety or both. The cyclic compounds producedin the process of the invention have two oxygen atoms single bonded tothe same carbon atom in the ring structure. Suitable cyclic acetal andketal moieties include 1,3-dioxolane moieties and 1,3-dioxane moieties,although larger ring compounds having oxygen atoms in the 1,3 positionare also contemplated.

The cyclic compounds produced in the process of the invention thatincludes a cyclic acetal moiety or a cyclic ketal moiety may berepresented by the general Formula II:

-   -   wherein R¹, R², R³, and R⁴ are independently H; a branched or        un-branched C₁-C₅₀ alkyl, C₂-C₅₀ alkenyl, aryl-C₁-C₅₀ alkyl,        aryl-C₂-C₅₀ alkenyl-, C₃-C₁₂ cycloalkyl, or a C₃-C₅₀ carboxylate        ester; and wherein R¹ and R² may optionally be bonded to each        other through one or more carbon atoms, and wherein R¹, R², R³,        and R⁴ optionally containing 1, 2, or 3 oxygen atoms in the        alkyl or alkenyl group, and wherein the alkyl, alkenyl, aryl,        and cycloalkyl groups of R¹, R², R³, and R⁴ are optionally        substituted with 1, 2, or 3 groups independently selected from        —OH, halogen, dialkylamino, aldehyde, ketone, carboxylic acid,        ester, ether, alkynyl, dialkylamide, anhydride, carbonate,        epoxide, lactone, lactam, phosphine, silyl, thioether, thiol,        and phenol;    -   wherein any one or both of R³ and R⁴ are optionally        independently a hydroxyl, halogen, dialkylamino, amine,        aldehyde, ketone, carboxylic acid, ester, ether, alkynyl,        dialkylamide, anhydride, carbonate, epoxide, lactone, lactam,        phosphine, silyl, thioether, thiol, or phenol;    -   wherein R⁵ is branched or unbranched divalent alkyl or divalent        alkenyl group each having 1 to 20 carbon atoms and optionally        containing 1, 2, or 3 oxygen atoms in the alkyl or alkenyl group        and optionally substituted with —OH, halogen, dialkylamino,        aldehyde, ketone, carboxylic acid, ester, ether, alkynyl, aryl,        dialkylamide, anhydride, carbonate, epoxide, lactone, lactam,        phosphine, silyl, thioether, thiol, and phenol; and    -   wherein n is an integer selected from 0 or 1.

R¹, R², R³, and R⁴ may independently be H, or a branched or un-branchedC₁-C₆ alkyl group. Or, R¹, R², R³, and R⁴ may independently be H, or abranched or un-branched C₁-C₄ alkyl group. R¹ may be a branched orunbranched C₁-C₆ alkyl group while R² is a hydrogen atom to provide acyclic acetal.

R⁵ may be a branched or unbranched divalent alkyl group having 1 to 6,or 1 to 4, or 1 to 3, or 1 to 2 carbon atoms.

Particularly useful cyclic acetals for this invention leading to usefulmaterials of commerce include 1,3-dioxolanes having R¹ being an alkylgroup that can lead to “E-series” type solvents. Likewise,1,3-dioxolanes having R1 being an alkyl group and R³ being a methylgroup can lead to “P-series” type solvents.

Examples of cyclic acetals include 2-propyl-1,3-dioxolane,2-propyl-1,3-dioxane, 2-ethyl-1,3-dioxolane, 2-ethyl-1,3-dioxane,2-methyl-1,3-dioxolane, 2-methyl-1,3-dixoane,2-propyl-4-methyl-1,3-dioxane, 5,5-dimethyl-2-propyl-1,3-dioxane,5,5-dimethyl-2-ethyl-1,3-dioxane, 2-ethyl-1,3-dioxepane,2-ethyl-1,3,6-trioxocane, 4-methanol-2-propyl-1,3-dioxolane, or4-methanol-2-propyl-1,3-dioxane, 4-methanol-2-propyl-1,3-dioxolane, and2-propyl-1,3-dioxane-4-ol.

Examples of cyclic ketals include 2,2-dimethyl-1,3-dioxolane,2,2-dimethyl-1,3-dioxane, 2,2,4-trimethyl-1,3-dioxolane,2,2-dimethyl-1,3-dioxepane, 4-methanol-2,2-dimethyl-1,3-dioxane,2,2-dimethyl-1,3-dioxan-4-ol, 2,2-dimethyl-1,3-6-trioxocane,2-isopropyl-2-methyl-1,3-dioxolane, 2-isopropyl-2-methyl-1,3-dioxane,2-isopropyl-2,4-dimethyl-1,3-dioxolane,2-isopropyl-2-methyl-1,3-dioxepane,4-methanol-2-isopropyl-2-methyl-1,3-dioxane,2-isopropyl-2-methyl-1,3-dioxan-4-ol,2-isopropyl-2-methyl-1,3-6-trioxocane, 2-methyl-2-pentyl-1,3-dioxolane,2-methyl-2-pentyl-1,3-dioxane, 2,4-dimethyl-2-pentyl-1,3-dioxolane,2-methyl-2-pentyl-1,3-dioxepane,2-methyl-2-pentyl-4-methanol-1,3-dioxolane,2-methyl-2-pentyl-1,3-dioxan-4-ol, 2-methyl-2-pentyl-1,3-6-trioxocane,

The reaction proceeds in the presence of a solid acid which remainssolid under reaction conditions. The solid acid is desirably a Brønstedacid or contains Brønsted acid sites. The reaction can proceed, forexample, in the presence of a solid ion exchange resin, desirably asolid acidic ion exchange resin. The solid acid can be a weak or strongacid. Strongly acidic ion exchange resins such as macroreticulatedpolymeric material derived from styrene or styrene and acrylic resins,such as divinylbenzene, containing pendant sulfonic acid groups aresuitable. Examples of such resins include those available from DowChemical Company and those formerly offered by Rohm and Haas,commercially available under the trade names of Amberlyst and Amberlite.For example, suitable ion exchange resins include Amberlyst® 15,Amberlyst 15DRY, Dowex® Monosphere 99 H, and Lewatit® M S100, SP112,K1221, and K2641, available from Bayer A G. Other solid acids includepolymers containing acid functionality such as sulfonated polymers, asexamples Amberlyst, Dowex, Smopex (polypropylene polymer manufactured byJohnson Matthey), Nafion (PTFE polymer), alumina, silica, mixtures ofsilica and alumina, zeolites, such as ZSM-5, aluminum phosphates,titanium oxides, tungsten on silica, heteropoly acids such asphosphomolybdates or phosphovanidates, and zirconia.

The reaction mixture is not treated to separate water from the reactionmixture prior to withdrawing the reaction mixture from the reactionzone. The reaction zone is liquid full with the liquid in the reactionzone being well mixed or proceeding in plug flow. The reactiontemperature is no particularly limited. The reaction conditions insidethe reaction zone desirably keep the reaction mixture in a liquid stateand are not set to exceed the boiling point of any ingredients under thereaction conditions. Suitable reaction temperatures are at least −15°C., or at least 0° C., or at least 15° C., or at least 25° C., or atleast 30° C., or at least 40° C., or at least 50° C. and desirably lessthan 110° C., up to 100° C., or up to 90° C., or up to 80° C.

The reaction mixture is withdrawn from the reaction zone as a liquidproduct stream line 4 as illustrated in FIG. 1. The product stream isconsidered a liquid product stream if water, cyclic compounds, andpolyhydroxyl compounds are present in the product stream as a liquid andhave not been subjected to temperatures above their boiling points inthe reaction zone under reaction zone conditions.

The liquid product stream removed from the reaction zone is also aunique composition. There is now provided a liquid compositioncomprising water, polyhydroxyl compounds, and cyclic compounds, each inthe following mole percentages based on the moles of all liquids in thecomposition:

-   -   a. water: at least 2 mole %, or at least 3 mole %, or at least 6        mole %, or at least 9 mole %, or at least 12 mole %, and up to        35 mole %, or up to 25 mole %, or up to 20 mole %, or up to 18        mole %;    -   b. polyhydroxyl compounds: at least 50 mole %, or at least 60        mole %, or at least 70 mole %, or at least 75 mole %, or at        least 80 mole %, and up to 95 mole %, or up to 90 mole %;    -   c. cyclic compounds: at least 2 mole %, or at least 3 mole %, or        at least 6 mole %, or at least 9 mole %, or at least 12 mole %,        and up to 35 mole %, or up to 25 mole %, or up to 20 mole %, or        up to 18 mole %;        wherein the liquid composition optionally contains carbonyl        compounds which, if present, do not exceed 20% of the number of        moles of cyclic compounds, and wherein the cumulative amount of        all liquid ingredient in the liquid composition other than a),        b), c), and carbonyl compounds, if present, does not exceed 10        mole %, and the cyclic compounds comprise cyclic acetals, cyclic        ketals, or a combination thereof.

The liquid composition optionally contains carbonyl compounds (i.e.aldehyde and/or ketone compounds) which, if present, do not exceed acumulative amount of 10%, or do not exceed 5%, of the number of moles ofcyclic compounds, and wherein the amount of any other liquid ingredientin the liquid composition does not exceed 8 mole %, or does not exceed 5mole %.

The cyclic compound in the liquid product stream may be a cyclic acetalor a cyclic ketal. The liquid product stream line 4 is fed directly orindirectly to a distillation column to separate the cyclic compounds andwater as one or more overhead product streams and unreacted polyhydroxylcompounds as one or more bottoms streams. The overhead product stream(s)may be a single overhead product stream as shown in line 5 of FIG. 1 ormultiple overhead product streams. The overhead product stream(s)exiting the distillation column is desirably a vapor stream(s). At leasta portion of the condensable compounds in these vapor streams aredesirably condensed for use as reflux and/or to isolate useful cyclicacetal products and thereafter purify the concentration of the liquidcyclic acetal products through conventional concentration and/orseparation techniques. As shown in FIG. 1, the distillation column hasan overhead product stream line 5, which is desirably a vapor whenexiting the distillation column and may be condensed if desired. Theoverhead product stream exiting the column is rich in the concentrationby weight of cyclic compounds relative to the concentration by weight ofcyclic compounds present in bottoms stream, or in other words, thequantity of cyclic compounds in the overhead product stream is greaterthan the quantity of cyclic compounds withdrawn from the distillationcolumn as a bottoms stream. It is preferred that the same holds true forwater in that water is present in the overhead product stream and theoverhead product stream is rich in concentration relative to theconcentration in the bottoms stream. By rich is meant a higherconcentration (in mole %) in one stream than the concentration of thesame ingredient in the comparative stream, and that the concentration ismeasured against all compounds which condense at 0° C. or higher(condensables). While the overhead product stream may contain unreactedpolyhydroxyl compounds, the overhead product stream is depleted(concentration by moles is less) in the quantity of this ingredientrelative to its quantity (concentration by moles) present in the bottomsstream. Thus, the bottoms stream is enriched in the number of unreactedpolyhydroxyl compounds relative to the number present in the overheadproduct stream. The bottoms stream exits the distillation column as aliquid stream. The bottoms stream may also contain by-products otherthan water. It is desirable that if by-products are present, that thequantity present in the bottoms stream is greater than the quantity inthe overhead product stream.

The number of theoretical stages or plates in the distillation columncan be from about 5 to about 100, or about 10-30 plates.

The overhead product stream can be subjected to condensation in acondenser. The condensate is collected in receiver or reflux drum andoptionally separated by any conventional means, such as a decanter. Theupper organic rich phase of the condensate in the receiver is withdrawnand recovered as product and can be further processed and purified toisolate a purified cyclic compound stream. The lower phase of thereceiver is water rich, withdrawn from the receiver, and sent to a watertreatment facility or further processed. Instead of a condenser, theoverhead product stream can be fed to a second distillation column toseparate water and unreacted carbonyl compounds from the desired cycliccompounds.

Table 1 below illustrates the mole % ranges (concentration ranges) foreach ingredient in the overhead product stream removed from thedistillation column train and after decanting (including the combinationof the aqueous and organic phases), wherein the stated mole % is basedon the weight of all ingredients within the overhead stream:

TABLE 1 Ingredient Mole % Mole % Mole % Water 30-50% 47-50%   48-49%Unreacted Carbonyl 0.1-20%  0.2-5% 1.5-2.0% Compounds By-Products  0-10%0-1.0% 0.4-0.6% Cyclic Compounds 30-50% 47-50%  48.5-49.5%  (acetals,ketals, or a combination) Polyhydroxyl  0-20% 0-1.0% 0.4-0.6% Compounds

The values in Table 1 above also apply to the mole % ranges for eachingredient in the overhead product stream, wherein the stated molepercentages are based on the cumulative moles of all fresh feedsentering the process.

The product stream exiting the reaction zone may optionally be subjectedto one or more process steps prior to entering the distillation column.For example, if a mobile solid acid catalyst is used, the product streamcan be filtered to remove the solid catalyst prior to distillation.

The bottoms stream 6 can be subjected to further process steps ifdesired. For example, the unreacted polyhydroxyl compounds present inthe bottoms stream may be separated from the bottoms stream by anyconventional separation technique. One such advantageous technique isfeeding the bottoms stream to a settling tank and phase separating theunreacted polyhydroxyl compounds from the by-products. The by-productsadvantageously phase separate as a top layer and can be decanted andremoved from the bottom polyhydroxyl layer as a by-product stream 7while the bottom polyhydroxyl layer can be removed at a location belowthe by-product layer such as depicted in streams 9 and 10.Alternatively, the bottoms stream may be subjected to an extractionseparation technique whereby a hydrocarbon extractant acting as asolvent for the more hydrophobic by-products is mixed with the bottomsstream to assist in the separation of the by-products stream. Forexample, organic solvents may be used in the extraction of byproductsand introduced into an extraction zone through stream 8. Suitablesolvents include liquid hydrocarbons with four carbons to more thantwenty carbons, saturated and unsaturated, with or without cyclicstructures, aliphatic and cyclic ethers, esters, fatty acids,halogenated hydrocarbons, aliphatic nitriles, and aliphatic and aromaticamines. Specific examples of organic solvents include heptane, octane,and nonane.

Often the polyhydroxyl compounds are separated from the bottoms stream,at least a portion can be recycled back to the reaction zone. As shownin FIG. 1, stream 10, a portion or all of the polyhydroxyl compoundsseparated from the bottoms stream and exiting the mixer/settler vesselare returned to a mixing zone feeding the reaction zone. It is desirableto feed the recycle stream 10 to the mixing zone if a mixing zone ispresent to uniformly disperse the carbonyl compounds in the polyhydroxylcomposition. A portion of the polyhydroxyl compounds separated from thebottoms stream may be purged through stream 9 and further processed topurify and re-use the purge stream.

The process of the invention is capable of producing a cyclic compoundyield of at least 90%, or at least 91%, or at least 92%, or at least93%, or at least 94%, or at least 95%, or at least 96%, or at least 97%,and up to 100%, or up to 99.5%, or up to 99%, or up to 98.5%, or up to98% based on the amount of aldehyde compounds fed to the reaction zone.The yield can be conveniently determined by measuring the production ofcyclic compounds in the overhead product stream removed from thedistillation column.

It is desirable to convert at least 90%, or at least 91%, or at least92%, or at least 93%, or at least 94%, or at least 95%, or at least 96%,or at least 97%, or at least 98%, or at least 99%, and up to 100%, or upto 99.5%, or up to 99% of the aldehyde compounds.

The selectivity to the cyclic compounds can be at least 90%, or at least91%, or at least 92%, or at least 93%, or at least 94%, or at least 95%,or at least 96%, or at least 97%, or at least 98%, or at least 99%, andup to 100%, or up to 99.5%, or up to 99%.

The process of the invention may be run in a batch mode, asemi-continuous mode, or a continuous mode. In a continuous mode and ina steady state operation, the process of the invention has a capacity ofproducing at least 70 metric tons/yr of cyclic compounds, or at least85, or at least 90, or at least 110 metric tons/yr.

The cyclic compounds in the separated cyclic compound stream can beconverted through hydrogenolysis to provide the corresponding etheralcohol solvents. For example, the following cyclic acetals2-propyl-1,3-dioxolane, 2-propyl-1,3-dioxane, 2-ethyl-1,3-dioxolane,2-ethyl-1,3-dioxane, 2-methyl-1,3-dioxolane, 2-methyl-1,3-dioxane,5,5-dimethyl-2-propyl-1,3-dioxane, 2-ethyl-1,3-dioxepane,2-ethyl-1,3,6-trioxocane, 4-methanol-2-propyl-1,3-dioxolane, or2-propyl-1,3-dioxane-4-ol, are suitable to make their respectivesolvents ethylene glycol monobutyl ether, 3-butoxy-1-propanol, ethyleneglycol monopropyl ether, 3-propoxy-1-propanol, ethylene glycol monoethylether, 3-ethoxy-1-propanol, 3-butoxy-2,2-dimethyl-1-propanol,4-propoxy-1-butanol, and diethylene glycol monobutyl ether,3-butoxy-1,2-propanediol, and 2-butoxy-1,3-propanediol throughhydrogenolysis.

EXAMPLES

The following apparatus was used for Examples 1-7. A glass, jacketedvessel was used as the reactor. It was maintained as liquid full byusing an up-flow orientation. The solid catalyst was contained in thereactor. A distillation column was also used. The distillation columnhad two sections each being 1″ vacuum-jacketed glass columns filled with0.24″ Pro-Pak distillation random packing. The upper section had 15″ ofpacking, while the lower section had 30″ of packing. The bottom reboilerwas a 1-liter glass, hot-oil jacketed vessel attached to the bottom ofthe lower column section. The top of the upper section was connected toa glass, jacketed, reflux splitter with a magnetic swing-arm controllerand a glass, jacketed condenser. The attached vent hose was connected toan ice trap, pressure controller, and vacuum pump. Vacuum-hose tubingwas used to connect equipment. The liquid stream from the column basewas connected by tubing to a positive displacement pump.

The tubing from the discharge of this pump was connected to a sectionwhich had two embodiments: a settler and an extractor. Each will bedescribed. As a settler, tubing from the positive displacement pump wasconnected to a 120-ml glass, jacketed vessel. This vessel had two exitports, one on the top and one on the bottom. During operations, it wasmaintained liquid full. The top port was connected to another positivedisplacement pump capable of removing byproduct material. The bottomport was connected by tubing to feed-material pumps described shortly.As an extractor, a glass feed vessel contained a solvent, e.g. octane.This solvent feed vessel was connected to a positive displacement pump.The tubing from this pump and the tubing from column bottom pump areconnected together. This combined stream was connected to a glass, 30-mlvessel maintained liquid-full which contained a magnetically-drivenstirrer. This mixed stream was connected to a 120-ml glass, jacketedvessel. This vessel had two exit ports, one on the top and one on thebottom. During operations, it was maintained liquid full. The top portwas connected to another positive displacement pump capable of removingmaterial enriched in byproduct material. The bottom port was connectedby tubing to feed-material pumps described below.

Glass feed vessels were used which contained aldehyde compound feedmaterial and polyhydroxyl compound feed material, separately. Each wasconnected by tubing to its own positive displacement pump. Tubing fromthese two feed-material pumps and tubing from the settler/extractor wereconnected together. The combined stream from these pumps was connectedto a glass, 30-ml liquid-full vessel which contained amagnetically-driven stirrer. A top exit port from the 30-ml vessel wasconnected to be bottom of the reactor vessel, completing the liquidcircuit. A process control system was utilized to monitor temperaturesand pump flow rates, and control the distillation column reflux splitterusing a column temperature set point. Nominal rates were 1 ml/min forfresh aldehyde compound feed, 1 ml/min for fresh polyhydroxyl compoundfeed, and 8 ml/min for unconverted recycled material.

When AMBERLYST® 15DRY was used as catalyst, it was prepared as follows.It was rinsed in DI water three times, and allowed to stand for one houror more in the polyhydroxyl compound. It was filtered and charged to thereactor.

In the examples given, the aldehyde used is n-butyraldehyde, and thepolyhydroxyl compound is ethylene glycol.

Example 1 AMBERLYST® 15DRY Catalyst, 50-ml Reactor, No Settler orExtractor

AMBERLYST® 15DRY was prepared as described above and loaded into a 50-mlglass reactor. The reactor jacket oil-bath temperature was set to 45° C.No settler or extractor was installed. The process ran for 60 hourscontinuously, and samples were taken periodically. The conversion datashowed no decrease, indicating no loss in catalyst activity. The overallconversion, selectivity, and yield were high: 93.1%, 99.0%, and 92.2%,respectively.

Example 2 AMBERLYST® 15DRY Catalyst, 100-ml Reactor, No Settler orExtractor

AMBERLYST® 15DRY was prepared as described above and loaded into a100-ml glass reactor. The reactor jacket oil-bath temperature was set to45° C. No settler or extractor was installed. The process ran for 70hours continuously, and samples were taken periodically. The conversiondata showed no decrease, indicating no loss in catalyst activity. Theoverall yield overall conversion, selectivity, and yield were high:98.0%, 99.4%, and 97.4%, respectively.

Example 3 AMBERLYST® 15DRY Catalyst, 150-ml Reactor, No Settler orExtractor

AMBERLYST® 15DRY was prepared as described above and loaded into a150-ml glass reactor. The reactor jacket oil-bath temperature was set to45° C. No settler or extractor was installed. The process ran for 76hours continuously, and samples were taken periodically. The conversiondata showed no decrease, indicating no loss in catalyst activity. Theoverall conversion, selectivity, and yield were high: 97.7%, 99.4%, and97.1%, respectively.

Example 4 AMBERLYST® 15DRY Catalyst, 150-ml Reactor, Heptane SettlerWithout Mixer

AMBERLYST® 15DRY was prepared as described above and loaded into a150-ml glass reactor. Using a pump, heptane was added intermittentlyinto the mixer, and a heptane-rich stream enriched in reactionbyproducts was pumped and removed from the top of the settler. Thereactor jacket oil-bath temperature was set to 45° C. A 15-ml settlerwas installed in the settler zone, but no 30-ml mixer was installed. Theprocess ran for 97 hours continuously, and samples were takenperiodically. The conversion data showed no decrease, indicating no lossin catalyst activity. The overall conversion, selectivity, and yieldwere high: 98.0%, 99.5%, and 97.5%, respectively.

Example 5 AMBERLYST® 15DRY Catalyst, 150-ml Reactor, Mixer-Settler withHeptane Solvent

AMBERLYST® 15DRY from Example 4 was re-used. The reactor jacket oil-bathtemperature was set to room temperature (22° C.). A 30-ml mixer followedby a 120-ml settler was installed in the separation zone. Using a pump,heptane was added intermittently into the mixer, and a heptane-richstream enriched in reaction byproducts was removed from the top of thesettler. The process ran for 96 hours continuously, and samples weretaken periodically. Since the catalyst was re-used from the previousexample, the accumulated catalyst operating time was 97-193 hours. Theconversion data showed no decrease, indicating no loss in catalystactivity. The overall conversion, selectivity, and yield were high:98.2%, 99.5%, and 97.7%, respectively.

Example 6 AMBERLYST® 15DRY Catalyst, 50-ml Reactor, Mixer-Settler withOctane Solvent

AMBERLYST® 15DRY from Example 5 was re-used. The reactor jacket oil-bathtemperature was set to room temperature (22° C.). A 30-ml mixer followedby a 120-ml settler was installed in the separation zone. Using a pump,octane was added intermittently into the mixer, and an octane-richstream enriched in reaction byproducts was removed from the top of thesettler. The process ran for 71 hours continuously. Because the catalystwas re-used from the previous example, the accumulated catalystoperating time was 193-264 hours. The conversion data showed nodecrease, indicating no loss in catalyst activity. The overallconversion, selectivity, and yield were high: 97.8%, 99.3%, and 97.1%,respectively.

Example 7 AMBERLYST® 15DRY Catalyst, 100-ml Reactor, Settler, No Mixeror Solvent

AMBERLYST® 15DRY was prepared as described above and loaded into a100-ml glass reactor. The reactor jacket oil-bath temperature was set toroom temperature (22° C.). No mixer or solvent was used. A 120-mlsettler was installed in the separation zone. A second, less-denseliquid phase was occasionally, intermittently removed from the top ofthe settler. The settler jacket set-point temperature was 60° C. Theprocess ran for 562 hours continuously, and samples were takenperiodically. The conversion data showed no decrease, indicating no lossin catalyst activity. The overall conversion, selectivity, and yieldwere high: 96.8%, 98.0%, and 94.9% respectively.

What we claim is:
 1. A process for making a cyclic compound compositioncomprising: a. feeding a carbonyl composition comprising an aldehydecompound, a ketone compound, or a combination thereof, and apolyhydroxyl composition comprising a polyhydroxyl compound, to areaction zone at a molar ratio of all polyhydroxyl compounds to allcarbonyl compounds fed to the reaction zone of at least 3:1; and b.reacting the carbonyl composition with the polyhydroxyl compound in thepresence of a solid acid to generate a liquid reaction mixturecomprising cyclic compounds, water, and unreacted polyhydroxylcompounds; and c. without separating water from the reaction mixture asit is being formed in the reaction mixture, withdrawing the liquidreaction mixture from the reaction zone as a liquid product stream; andd. feeding the liquid reaction product stream directly or indirectly toa distillation column to separate cyclic compounds from unreactedpolyhydroxyl compounds and withdrawing from the distillation column anoverhead product stream and a bottoms stream, wherein the overheadproduct stream comprises cyclic compounds, unreacted polyhydroxylcompounds and water and is rich in the concentration of cyclic compoundsby moles relative to the bottoms stream, and the bottoms streamcomprises unreacted polyhydroxyl compounds and is rich in theconcentration of unreacted polyhydroxyl compounds by moles relative tothe overhead product stream; wherein the selectivity to cyclic compoundsin the overhead product stream is at least 90%.
 2. The process of claim1, wherein at least a portion of unreacted polyhydroxyl compounds arerecycled back to the reaction zone.
 3. The process of claim 1, whereinthe bottoms stream further comprises reaction by-products, and whereinthe reaction by-products are separated from unreacted polyhydroxylcompounds to produce a polyhydroxyl rich stream and a by-product richstream.
 4. The process of claim 1, wherein the carbonyl compositioncomprises carbonyl compounds represented by Formula I:

in which R¹ and R² are independently hydrogen or a C₁-C₅₀ alkyl, C₂-C₅₀alkenyl, aryl-C₁-C₅₀ alkyl, aryl-C₂-C₅₀ alkenyl, or C₃-C₁₂ cylcoalkyl,and wherein R¹ and R² are optionally connected through one or morecarbon atoms, and wherein the alkyl, alkenyl, aryl, and cycloalkylgroups of R¹ and R² are optionally saturated or unsaturated, andbranched or unbranched, or substituted or unsubstituted with 1, 2, or 3groups comprising —OH, halogen, dialkylamino, C₁-C₆ alkyl, aldehyde,ketone, carboxylic acid, ester, ether, alkynyl, dialkylamide, anhydride,carbonate, epoxide, lactone, lactam, phosphine, silyl, thioether, thiol,aryl, phenol, or combinations thereof.
 5. The process of claim 4,wherein the carbonyl compounds comprise benzaldehyde, acetaldehyde,propionaldehyde, butyraldehyde, isobutyraldehyde, pentaldehyde,2-methylbutyraldehyde, 3-methylbutyraldehyde, n-pentanal, isopentanal,hexyldehyde, heptaldehyde, 2-ethylhexyldehyde, octanal, nonanal,n-decanal, 2-methylundecanal, lauryl aldehyde, myristyl aldehyde, cetylaldehyde, stearyl aldehyde, behenyl aldehyde, glutaraldehyde, acrolein,crotonaldehyde, oleyl aldehyde, linoleyl aldehyde, linolenyl aldehyde,erucyl aldehyde, cinnamaldehyde, 1,3-cyclohexanedicarboxaldehyde,1,4-cyclohexanedicarboxaldehyde, or combinations thereof.
 6. The processof claim 4, wherein the polyhydroxyl compounds comprise ethylene glycol,1,2-propanediol, 1,3-propanediol, 1,4-butanediol, 1,3-butanediol,1,2-butanediol, 1,2-pentanediol, 2,4-pentandiol,2,2-dimethyl-1,3-propanediol, diethyleneglycol, and triethyleneglycol,glycerin, trimethylolpropane, xylitol, arabitol, 1,2- or1,3cyclopentanediol, 1,2- or 1,3-cyclohexanediol, 2,3-norbornanediol, orcombinations thereof.
 7. The process of claim 4, wherein the carbonylcompounds comprise propionaldehyde, butyraldehyde, isobutyraldehyde,2-ethylhexyldehyde, 1,3-cyclohexanedicarboxaldehyde,1,4-cyclohexanedicarboxaldehyde, or combinations thereof, and thepolyhydroxyl compound comprises ethylene glycol, 1,2-propanediol,1,3-propanediol, 1,4-butanediol, 1,3-butanediol, 1,2-butanediol,diethyleneglycol, or combinations thereof.
 8. The process of claim 4,wherein the carbonyl compounds comprise acetone, methyl ethyl ketone(2-butanone), methyl propyl ketone (2-pentanone), methyl isopropylketone (3-methyl-2-butanone), methyl isobutyl ketone(4-methyl-2-pentanone), 2-hexanone, 2-heptanone (methyl amyl ketone),2-octanone, and acetophenone.
 9. The process of claim 1, wherein saidmolar ratio is at least 5:1.
 10. The process of claim 1, wherein thecarbonyl compounds and the polyhydroxyl compounds are premixed togetherprior to entry into the reaction vessel.
 11. The process of claim 1,wherein the reaction vessel contains a fixed bed of solid acid.
 12. Theprocess of claim 11, wherein the reaction zone is liquid full.
 13. Theprocess of claim 12, wherein the reaction mixture flows in an upwarddirection in a vertically oriented reaction zone.
 14. The process ofclaim 13, wherein the reaction vessel is a pipe.
 15. The process ofclaim 1, wherein the cyclic compounds contain a moiety represented bythe Formula II:

wherein R¹, R², R³, and R⁴ are independently H; a branched orun-branched C₁-C₅₀ alkyl, C₂-C₅₀ alkenyl, aryl-C₁-C₅₀ alkyl, aryl-C₂-C₅₀alkenyl-, C₃-C₁₂ cycloalkyl, or a C₃-C₅₀ carboxylate ester; and whereinthe alkyl, alkenyl, aryl, and cycloalkyl groups of R¹, R², R³, and R⁴,wherein R¹ and R² may optionally be bonded to each other through one ormore carbon atoms, and wherein R¹, R², R³, and R⁴ optionally containing1, 2, or 3 oxygen atoms in the alkyl or alkenyl group, and optionallysubstituted with 1, 2, or 3 groups independently selected from —OH,halogen, dialkylamino, aldehyde, ketone, carboxylic acid, ester, ether,alkynyl, dialkylamide, anhydride, carbonate, epoxide, lactone, lactam,phosphine, silyl, thioether, thiol, and phenol; wherein any one or bothof R³ and R⁴ are optionally independently a hydroxyl, halogen,dialkylamino, amine, aldehyde, ketone, carboxylic acid, ester, ether,alkynyl, dialkylamide, anhydride, carbonate, epoxide, lactone, lactam,phosphine, silyl, thioether, thiol, or phenol; wherein R⁵ is branched orunbranched divalent alkyl or divalent alkenyl group each having 1 to 20carbon atoms and optionally containing 1, 2, or 3 oxygen atoms in thealkyl or alkenyl group and optionally substituted with —OH, halogen,dialkylamino, aldehyde, ketone, carboxylic acid, ester, ether, alkynyl,aryl, dialkylamide, anhydride, carbonate, epoxide, lactone, lactam,phosphine, silyl, thioether, thiol, and phenol; and wherein n is aninteger selected from 0 or
 1. 16. The process of claim 1, wherein thecyclic compounds comprise 2-propyl-1,3-dioxolane, 2-propyl-1,3-dioxane,2-ethyl-1,3-dioxolane, 2-ethyl-1,3-dioxane, 2-methyl-1,3-dioxolane,2-methyl-1,3-dixoane, 2-propyl-4-methyl-1,3-dioxane,5,5-dimethyl-2-propyl-1,3-dioxane, 5,5-dimethyl-2-ethyl-1,3-dioxane,2-ethyl-1,3-dioxepane, 2-ethyl-1,3,6-trioxocane,4-methanol-2-propyl-1,3-dioxolane, or 4-methanol-2-propyl-1,3-dioxane,or combinations thereof.
 17. The process of claim 1, wherein the solidacid comprises an acidic ion exchange resin.
 18. The process of claim 1,wherein the reaction conditions within the reaction zone retain thereaction mixture in a liquid state and are not set to exceed the boilingpoint of any ingredients in the reaction mixture under the operatingconditions of the reaction zone.
 19. The process of claim 1, wherein thetemperature in the reaction zone ranges from −15° C. to 110° C.
 20. Theprocess of any one of claims 1-19, wherein the process is continuous andthe yield of cyclic compounds is at least 95%.
 21. The process of claim1, wherein the yield of cyclic compounds in the overhead product streamis at least 90%.